FI128139B

FI128139B - Production of hydrocarbons from recycled or renewable organic material

Info

Publication number: FI128139B
Application number: FI20185653A
Authority: FI
Inventors: Jouni Touronen; Kaisa Lamminpää; Antti Pasanen; Susanna Kuitunen; Anna Zaitseva
Original assignee: Neste Oyj
Priority date: 2018-07-20
Filing date: 2018-07-20
Publication date: 2019-10-31
Also published as: WO2020020771A1; EP3824047A1; US20210269722A1; FI20185653A1

Abstract

Provided herein is a method of producing hydrocarbons from a recycled or renewable organic material wherein the recycled or renewable organic material comprises hydroxyaromatic hydrocarbon compounds ,comprising the steps of (a) providing recycled or renewable organic material; (b) optionally purifying the recycled or renewable organic material; (c) hydrotreating the recycled or renewable organic material in a presence of a hydrotreating catalyst, thereby forming a hydrocarbon stream and a phenol-containing effluent; (d) separating phenols from the phenol-containing effluent of step (c), thereby forming a phenol stream and a purified water stream; and (e) recycling the phenol stream obtained in step (d) to step (c) to increase the yield of hydrocarbons obtained from step (c); to obtain hydrocarbons comprising less than 1 wt% oxygen.

Description

FIELD OF THE INVENTION

The present invention relates to a method of producing hydrocarbons from a recycled or renewable organic material, in particular recycled or renewable organic material comprising hydroxyaromatic hydrocarbon compounds.

BACKGROUND OF THE INVENTION

In some cases recycled or renewable organic material contains organic high amounts of complex organic molecules that degrade to phenol derivatives 10 when subjected to hydrotreatment processes. For example tall oil pitch (TOP) contains high amounts of sterols. In a hydrotreatment process, such as hydrodeoxygenation (HDO), the sterols degrade to, among others, low molar weight phenol and alkylphenols. The alkylphenols and phenol are water soluble and end up into the waste water stream reducing the potential hydrocarbon yield from the 15 process. Phenol yield from the hydrotreatment of TOP can be as high as 1 kg/ton of TOP. Such high yield of phenols is challenging for a waste water treatment plant because phenols are poisonous for a biological treatment. Therefore a strategy to handle the produced phenols is required.

BRIEF DESCRIPTION OF THE INVENTION

An object of the present invention is thus to provide a method so as to overcome the above problems. The objects of the invention are achieved by a method which is characterized by what is stated in the independent claims. The preferred embodiments of the invention are disclosed in the dependent claims.

The invention is based on the surprizing realization recycled or re25 newable organic material containing high amounts of hydroxyaromatic hydrocarbon compounds, such as phenolic compounds, may be used to produce hydrocarbons from recycled or renewable organic material while minimizing the amount of phenols in waste water by separating phenols from the phenol-containing effluent obtained from a hydrotreatment step and recycling said phenol stream 30 back to hydrotreatment step simultaneously increasing the yield of obtained hydrocarbons.

20185653 prh 20 -07- 2018

BRIEF DESCRIPTION OF THE DRAWINGS

In the following the invention will be described in greater detail by means of preferred embodiments with reference to the attached drawings, in which

Figure 1 illustrates a first exemplary process flow of the present method;

Figure 2 illustrates a second exemplary process flow of the present method;

Figure 3 is scheme for the separation of waste water in a HDO process; 10 Figure 4 is scheme of an extractive phenol separation process.

DETAILED DESCRIPTION OF THE INVENTION

The present invention provides a method of producing hydrocarbons from recycled or renewable organic material.

The term “recycled or renewable organic material refers to organic 15 material, i.e. material containing carbon, obtained 1) from a natural resource which replenishes to overcome recourse depletion caused by its usage and consumption or 2) from a raw or processed material that is recovered from a waste for reuse. The recycled or renewable organic material characteristically comprises aliphatic compounds having a carbon chain of from 4 to 30 carbon atoms, par20 ticularly from 12 to 22 carbon atoms. Typical examples of such aliphatic compounds are fatty acids or esters thereof, in particular wherein the fatty acids have an aliphatic chain of from 4 to 30 carbon atoms, more particularly from 12 to 22 carbon atoms. The recycled or renewable organic material typically comprises at least 50 wt% aliphatic compound of the total weight of the recycled or renewable 25 organic material.

Typically the recycled or renewable organic material refers to fats and/or oils of plant, microbial, algal, and/or animal origin. It also refers to any waste stream received from processing of such oils and/or fats. The recycled or renewable organic material may be in an unprocessed form (e.g. animal fat), or a 30 processed form (used cooking oil). The recycled or renewable organic material also refers to fossil waste-based oils and waste oils.

The term plant based fats and oils refers to fat and/or oils of plant origin i.e. oils that can originate directly from plants or can be byproducts from various industrial sectors, such as agriculture or forest industry.

20185653 prh 20 -07- 2018

Examples of plant based fats and oils of the present invention include, but are not limited to, sludge palm oil, rapeseed oil, canola oil, colza oil, sunflower oil, soybean oil, hemp oil, olive oil, linseed oil, cottonseed oil, mustard oil, palm oil, arachis oil, castor oil and coconut oil.

Other examples of plant based fats and oils include biocrudes and bio oils. Biocrudes and bio oils are produced from biomass, in particular from lignocellulosic biomass, with various liquefying methods, such as hydrothermal liquefaction, or pyrolysis, in particular fast pyrolysis.

The term biocrude refers to oils produced from biomass by employ10 ing hydrothermal liquefaction. The term bio oil refers to pyrolysis oils produced from biomass by employing pyrolysis. The term biomass refers to material derived from recently living organisms, which includes plants, animals and their byproducts. The term lignocellulosic biomass refers to biomass derived from plants or their byproducts. Lignocellulosic biomass is composed of carbohydrate 15 polymers (cellulose, hemicellulose) and an aromatic polymer (lignin).

The term pyrolysis refers to thermal decomposition of materials at elevated temperatures in a non-oxidative atmosphere. The term fast pyrolysis refers to thermochemical decomposition of biomass through rapid heating in absence of oxygen. The term hydrothermal liquefaction (HTL) refers to a thermal 20 depolymerization process used to convert wet biomass into crude-like oil under moderate temperature and high pressure.

Examples of bio oil and biocrude produced from lignocellulosic biomass, e.g. materials like forest harvesting residues or byproducts of a saw mill, are lignocellulosic pyrolysis liquid (LPL), produced by employing fast pyrolysis, 25 and HTL-biocrude, produced by employing hydrothermal liquefaction.

Further examples of plant based fats and oils include crude tall oil (CTO), obtained as a by-product of the Kraft process (wood pulping), and its derivatives, such as tall oil pitch (TOP), crude fatty acid (CFA), tall oil fatty acid (TOFA) and distilled tall oil (DTO).

Crude tall oil comprises resin acids, fatty acids, and unsaponifiables.

Resin acids are a mixture of organic acids derived from oxidation and polymerization reactions of terpenes. The main resin acid in crude tall oil is abietic acid but abietic derivatives and other acids, such as primaric acid are also found. Fatty acids are long chain monocarboxylic acids and are found in hardwoods and soft35 woods. The main fatty acids in crude tall oil are oleic, linoleic and palmitic acids. Unsaponifiables cannot be turned into soaps as they are neutral compounds

20185653 prh 20 -07- 2018 which do not react with sodium hydroxide to form salts. They include sterols, higher alcohols and hydrocarbons. Sterols are steroids derivatives which also include a hydroxyl group.

The term “tall oil pitch (TOP)” refers to residual bottom fraction from crude tall oil (CTO) distillation processes. Tall oil pitch typically comprises from to 51 wt% free acids, from 23 to 37 wt% esterified acids, and from 25 to 34 wt% unsaponifiable neutral compounds of the total weight of the tall oil pitch. The free acids are typically selected from a group consisting of dehydroabietic acid, abietic and other resin acids. The esterified acids are typically selected from 10 a group consisting of oleic and linoleic acids. The unsaponifiables neutral compounds are typically selected from a group consisting of diterpene sterols, fatty alcohols, sterols, and dehydrated sterols.

The term “crude fatty acid (CFA)” refers to fatty acid-containing materials obtainable by purification (e.g., distillation under reduced pressure, extracts tion, and/or crystallization) of CTO.

The term “tall oil fatty acid (TOFA)” refers to fatty acid rich fraction of crude tall oil (CTO) distillation processes. TOFA typically comprises mainly fatty acids, typically at least 80 wt% of the total weight of the TOFA. Typically TOFA comprises less than 10 wt% rosin acids.

The term “distilled tall oil (DTO)” refers to resin acid rich fraction of crude tall oil (CTO) distillation processes. DTO typically comprises mainly fatty acids, typically from 55 to 90 wt%, and rosin acids, typically from 10 to 40 wt% rosin acids, of the total weight of the DTO. Typically DTO comprises less than 10 wt% unsaponifiable neutral compounds of the total weight of the distilled tall oil.

The term animal based fats and oils” refers to fats and/or oils of animal origin i.e lipid materials derived from animals. Examples of animal based fats and oils include, but are not limited to, such as suet, tallow, blubber, lard, train oil, milk fat, fish oil, poultry oil and poultry fat.

The term “microbial oils” refers to triglycerides (lipids) produced by 30 microbes.

The term “algal oils” refers to oils derived directly from algae.

The term “fossil waste-based oils” refers to oils produced from waste streams like waste plastics or end-life-tires. Examples of fossil waste-based oils include waste plastic pyrolysis oil (WPPO) and end-life-tire pyrolysis oil (ELTPO).

The term “waste oils” refers to any oils that, through contamination, have become unsuitable for their original purpose due to the presence of impuri

20185653 prh 20 -07- 2018 ties or loss of original properties. Examples of waste oils are used lubricant oils (ULO), hydraulic oils, transformer oils or oils used in metal working.

In the present invention the recycled or renewable organic material is typically selected from a group consisting of plant based fats and oils, animal 5 based fats and oils, fossil waste-based oils, waste oils, algal oils and microbial oils.

Particular examples of the recycled or renewable organic material of the present invention include, but are not limited to, animal based fats and oils, such as suet, tallow, blubber, lard, train oil, milk fat, fish oil, poultry oil, and poultry fat; plant based fats and oils, such as sludge palm oil, rapeseed oil, canola oil, 10 colza oil, sunflower oil, soybean oil, hemp oil, olive oil, linseed oil, cottonseed oil, mustard oil, palm oil, arachis oil, castor oil, coconut oil, lignocellulosic pyrolysis liquid (LPL), HTL biocrude, crude tall oil (CTO), tall oil pitch (TOP), crude fatty acid (CFA), tall oil fatty acid (TOFA) and distilled tall oil (DTO); microbial oils; algal oils; recycled fats or various waste streams of the food industry, such as used 15 cooking oil, yellow and brown greases; free fatty acids, any lipids containing phosphorous and/or metals, oils originating from yeast or mold products, recycled alimentary fats; starting materials produced by genetic engineering, and any mixtures of said feedstocks.

In an example of the present invention the recycled or renewable or20 ganic material is selected from a group consisting of lignocellulosic biomass based oils such as lignocellulose pyrolysis liquid (LPL) and HTL-biocrude; crude tall oil and its derivatives; such as tall oil pitch (TOP), tall oil fatty acid (TOFA), distilled tall oil (DTO) and, crude fatty acid (CFA); sterol containing fats, such as animal fats; preferably the recycled or renewable organic material is crude tall oil (CTO) 25 or tall oil pitch (TOP).

In another example of the present invention the recycled or renewable organic material is selected from a group consisting of tall oil, tall oil distillation derivates, such as tall oil pitch (TOP), crude fatty acid (CFA), tall oil fatty acid (TOFA), distilled tall oil (DTO), and pyrolysis oils, such as hydrothermal liquefac30 tion oils (HTL) and lignocellulose pyrolysis oils; more particularly the recycled or renewable organic material is tall oil pitch (TOP).

The recycled or renewable organic material to be treated by the present method contains high amounts hydroxyaromatic hydrocarbon compounds. Examples of such hydroxyaromatic hydrocarbon compounds include plant based 35 hydroxyaromatic hydrocarbon compounds such as sterols, lignin, and phenolic lipids such as cardanol. Further examples of hydroxyaromatic hydrocarbon com6

20185653 prh 20 -07- 2018 pounds include animal fat based hydroxyaromatic hydrocarbon compounds such as sterols. The recycled or renewable organic material of the present invention comprises more than 0.01 wt% hydroxyaromatic hydrocarbon compounds. In particular the recycled or renewable organic material of the present invention 5 comprises more than 0.05 wt% hydroxyaromatic hydrocarbon compounds, more particularly the recycled or renewable organic material of the present invention comprises more than 0.1 wt% hydroxyaromatic hydrocarbon compounds, and even more particularly the recycled or renewable organic material of the present invention comprises more than 0.5 wt% hydroxyaromatic hydrocarbon com10 pounds of the total weight of the recycled or renewable organic material.

The recycled or renewable organic material to be treated by the present method may also comprise further impurities e.g. impurities comprising phosphorus and/or metals in the form of phospholipids, soaps and/or salts. The impurities may for example be in the form of phosphates or sulfates, iron salts or 15 organic salts, soaps or phospholipids. The metal impurities that may be present in the biomass-based lipid material are for example alkali metals or alkali earth metals, such as sodium or potassium salts, or magnesium or calcium salts, or any compounds of said metals.

Accordingly provided herein is a method of producing hydrocarbons 20 from recycled or renewable organic material wherein the recycled or renewable organic material comprises hydroxyaromatic hydrocarbon compounds, comprising the steps of (a) providing recycled or renewable organic material;

(b) optionally purifying the recycled or renewable organic material;

and (c) hydrotreating the recycled or renewable organic material in a presence of a hydrotreating catalyst, thereby forming a hydrocarbon stream and a phenol containing effluent; and (d) separating phenols from the phenol containing effluent of step (cj, 30 thereby forming a phenol stream and a purified water stream; and (e) recycling the phenol stream obtained in step (d) to step (cj to increase the yield of hydrocarbons obtained from step (c);

to obtain hydrocarbons comprising less than 1 wt% oxygen.

In step (b) the recycled or renewable organic material is optionally pu35 rifled to remove undesired impurities, such as phosphorous and/or silicon, from the recycled or renewable organic material. The purification step (b) may be ac

20185653 prh 20 -07- 2018 complished by heat treating or bleaching the recycled or renewable organic material or by any other method found suitable by a skilled person for purifying recycled or renewable organic material.

The recycled or renewable organic material is subjected to hydro5 treatment in a presence of a hydrotreating catalyst, optionally after the purification step (b).

The term “hydrotreating” refers to a chemical engineer process in which reaction of hydrogen is used to remove impurities, such as oxygen, sulphur, nitrogen, phosphorous, silicon and metals, especially as part of oil refining.

Hydrotreating can be performed in one or several steps in one or more reactor units or catalyst beds.

Step (c) is typically achieved under continuous hydrogen flow. For achieving optimal results the continuous hydrogen flow is step (c) preferably has H2/feed ratio from 500 to 2000 n-L/L, more preferably from 800 to 1400 n-L/L.

In step (c) hydrotreatment is advantageously performed at a temperature from 270 to 380°C, preferably from 275 to 360°C, more preferably from 300 to 350°C. Typically the pressure in step (c) is from 4 to 20 MPa.

The hydrotreatment catalyst is step (c) preferably comprises at least one component selected from 1UPAC group 6, 8 or 10 of the Periodic Table.. Pref20 erably the hydrotreating catalyst in step (c) is a supported Pd, Pt, Ni, NiW, NiMo or a CoMo catalysts and the support is zeolite, zeolite-alumina, alumina and/or silica, preferably N1W/AI2O3, NiMo/AhOs or CoMo/AhOs. In particular the hydrotreating catalyst is a sulphided NiW, NiMO or CoMo catalyst.

The time during which the recycled or renewable organic material is 25 heated and held at the desired temperature, i.e. residence time, is typically from 1 to 300 min, preferably from 5 to 240 min, more preferably from 30 to 90 min in step (c).

An applicable hydrotreatment step (c) provides a purified hydrotreated recycled or renewable organic material. The purified hydrotreated recycled or 30 renewable organic material advantageously comprises less than 50 % of the chlorine content of the recycled or renewable organic material provided in step (a).

For achieving optimal results part of the hydrotreated recycled or renewable organic material may be recycled in step (c). Preferably the ratio of the fresh feed i.e. purified recycled or renewable organic material obtained in step (b) 35 to the recycled hydrotreated recycled or renewable organic material is from 2:1 to 20:1.

20185653 prh 20 -07- 2018

In a particular example step (c) is accomplished by (cl) hydrodeoxygenating (HDO) the recycled or renewable organic material. This is preferably achieved in a presence of a HDO catalyst. Preferably this is achieved at a presence of a HDO catalyst at a temperature from 290 to 350°C under pressure from 4 to 5 20 MPa and under continuous hydrogen flow.

The term “hydrodeoxygenation (HDO)” refers to removal of oxygen as water by the means of molecular hydrogen under the influence of a (HDO) catalyst.

The HDO catalyst may for example be selected from a group consisting 10 of NiMO-, CoMo-, NiW-catalysts and any mixtures thereof. Preferably the HDO catalyst is sulphided NiW, NiMo or CoMo catalyst.

Advantageously, the continuous hydrogen flow has H2/feed ratio from 500 to 2000 n-L/L, preferably from 800 to 1400 n-L/L.

Preferably step (cl) is performed to obtain hydrodeoxygenated recy15 cled or renewable organic material comprising less than 1 wt% oxygen.

For achieving optimal results part of the deoxygenated recycled or renewable organic material may be recycled in step (c). Preferably the ratio of the fresh feed i.e. purified recycled or renewable organic material obtained in step (b) to the recycled deoxygenated recycled or renewable organic material is from 2:1 20 to 20:1.

In another example step (c) is accomplished by (c2) hydrodesulfurizing (HSD) the heat treated recycled or renewable organic material fraction. The term “hydrodesulfurisation (HDS)” refers to removal of sulfur as hydrogensulfide by the means of molecular hydrogen under the influence of a (HDS) catalyst.

In another example step (c) is accomplished by (c3) hydrometaillizing (HDM) the heat treated recycled or renewable organic material fraction. The term “hydrodemetallization (HDM)” refers to removal of metals by trapping them with a (HDM) catalyst.

In another example step (c) is accomplished by (c4) hydrodenitrificat30 ing (HDN) the heat treated recycled or renewable organic material fraction. The term “hydrodenitrification (HDN)” refers to removal of nitrogen by the means of molecular hydrogen under the influence of a (HDN) catalyst.

In another example step (c) is accomplished by (c5) hydrodearomatizing (HDA) the heat treated recycled or renewable organic material fraction. The 35 term “hydrodearomatisation (HDA)” refers to saturation or ring opening of aro

20185653 prh 20 -07- 2018 matics by the means of molecular hydrogen under the influence of a (HDA) catalyst.

In step (d) phenols are separated from the phenol containing effluent thereby forming a phenol stream and a purified water stream.

Step (d) may be accomplished by any viable physical separation method found suitable by a skilled person for separation phenol from an aqueous phase. Suitable examples include, but are not limited to stripping and liquid-liquid extraction. Preferably step (d) is accomplished by liquid-liquid extraction.

For another example (dl) the phenols are separated from the phenol 10 containing effluent by liquid-liquid extraction with a non-aromatic organic solvent that is sparingly soluble to water. Preferably the non-aromatic organic solvent is selected from a group consisting of mesityl oxide, methyl isobutyl ketone, methyl tert-butyl ketone, methyl tert-butyl ether, methyl isopropyl ketone, 3heptanone, 2-hexanone and mixtures thereof. More preferably the non-aromatic 15 organic solvent is methyl isobutyl ketone.

Step (dl) takes place at any temperature from 30 to 50°C and is performed under pressure from 100 to 200 kPa.

After separation in step (d) the phenol stream is recycled to the hydrodeoxygenation step (c) wherein it is converted to benzene and alkylbenzenes 20 and other cracking products under the prevailing conditions. This increases the hydrocarbon yield of the hydrotreatment process.

Figure 1 illustrates a first exemplary process flow of the present method.

Referring to Figure 1, a feed of recycled or renewable organic material, 25 in particular tall oil pitch (TOP), 10 is optionally subjected to a step of heat treating 20 the recycled or renewable organic material as discussed herein for step (bl). The heat treated feed of recycled or renewable organic material is then evaporated 30 as discussed herein for step (bl) and a bottom containing a heat treated recycled or renewable organic material fraction 31 comprising less than 30 50% of the original silicon content of the recycled or renewable organic material provided in step (a), and a vapor fraction 32 comprising the major part of volatile undesired impurities is obtained. The heat treated recycled or renewable organic material is then subjected to hydrotreatment 40, as discussed herein for step (c) to obtain a hydrocarbon stream 41 and a phenol containing effluent 42. The phe35 nol containing effluent is then subjected to separating 50 phenols from the phenol-containing effluent of step (d), thereby forming a phenol stream 51 and a pu

20185653 prh 20 -07- 2018 rified water stream 52 as discussed herein for step (d); and the phenol stream obtained in step (d) is then recycled to hydrotreatment 40 as discussed herein for step (e). The purified recycled or renewable organic material 41 may then be subjected to catalytic upgrading 60.

Figure 2 illustrates a second exemplary process flow of the present method.

Referring to Figure2, a feed of recycled or renewable organic material, in particular tall oil pitch (TOP), 10 is optionally subjected to a step of heat treating 25 the recycled or renewable organic material in a presence of an adsorbent 10 as discussed herein for step (b2). The adsorbent is then separated 35 from the heat treated feed of recycled or renewable organic material as discussed herein for step (b2) and a heat treated recycled or renewable organic material fraction 31 comprising less than 50% of the original silicon content of the recycled or renewable organic material provided in step (a), and the adsorbent 33 comprising 15 the major part of undesired impurities is obtained. The heat treated recycled or renewable organic material is then subjected to hydrotreatment 40, as discussed herein for step (c) to obtain a hydrocarbon stream 41 and a phenol containing effluent 42. The phenol containing effluent is then subjected to separating 50 phenols from the phenol-containing effluent of step (d), thereby forming a phenol 20 stream 51 and a purified water stream 52 as discussed herein for step (d); and the phenol stream obtained in step (d) is then recycled to hydrotreatment 40 as discussed herein for step (e). The purified recycled or renewable organic material 41 may then be subjected to catalytic upgrading 60.

After hydrocarbons have been produced in accordance with the pre25 sent method, it may be subjected to further processing e.g. catalytic upgrading.

Such catalytic upgrading processes include, but are not limited to, catalytic cracking, catalytic hydrocracking, thermo-catalytic cracking, catalytic hydrotreatment, fluid catalytic cracking, catalytic ketonization, and catalytic esterification. Such processes require the recycled or renewable organic material to be sufficiently 30 pure and free from impurities that may otherwise hamper the catalytic process or poison the catalyst(s) present in the process.

Accordingly the present invention further provides a process for producing recycled or renewable hydrocarbons, comprising steps of (x) purifying the recycled or renewable organic material as discussed herein, and (y) subjecting 35 the purified recycled or renewable organic material to an oil refinery conversion process, wherein the oil refinery conversion process comprises altering the mo

20185653 prh 20 -07- 2018 lecular weight of the feed, such hydrocracking, or steamcracking, removal of heteroatoms from the feed, such as thermal catalytic cracking, fluid catalytic cracking, or hydrotreating, in particular hydrodeoxygenating, or hydrodesulfurizing, altering the degree of saturation of the feed, such as hydrotreating, thermal cata5 lytic cracking, or fluid catalytic cracking, rearranging the molecular structure of the feed, such as isomerizing, or any combination thereof to obtain at least one recycled or renewable hydrocarbon.

In a typical example of the present process the recycled or renewable hydrocarbon is a renewable traffic fuel or fuel component.

In an example of the present process, step (y) is hydrocracking. In such example, step (y) is preferably performed in a mild hydrocracking (MHC) refinery unit, in particular in a presence of a hydrocracking catalyst.

In another example of the present process, step (y) is steamcracking.

In such example step (y) is preferably performed in a steamcracking unit.

In yet another example of the present process, step (y) is isomerization. In such example, step (y) is preferably performed in an isomerization unit.

In yet another example of the present process, step (y) is hydrotreating. In such example, step (y) is preferably performed in a hydrotreating unit.

In yet another example of the present process, step (y) is thermal cata20 lytic cracking (TCC). In such example, step (y) is preferably performed in a thermal catalytic cracking unit.

In yet another example of the present process, step (y) is fluid catalytic cracking (FCC). In such example, step (y) is preferably performed in a fluid catalytic cracking unit.

EXAMPLES

The test simulations were made to provide preliminary estimates for the cost of the phenol separation process. The waste water stream from Figure 3 is considered in the simulation and the update of other streams shown in Figure 3 is provided for the process with the phenol stream recycling.

For extraction process (Figure 4) the simulation is done for a 40C extraction process and the solvent recycle distillation at 1 bar. The conditions could be optimized in future, because there is overpressure in the feed water stream and the phenol recycle should be pressurized for the recycling to the reactor. The considered process is based on methyl isobutyl ketone solvent, which demon35 strates very high selectivity towards phenol extraction.

Table 1. Comparison of the phenol separation processes; phenol stripping and phenol extraction. Phenol flow rates.

Case	Recycle + phenol conversion	Phenol recycled	Phenol in rec. Oil	phenol in sour gas	Phenol in oil product	phenol in waste water	Phenol in waste water	Benzene yield
		kg/h	kg/h	kg/h	kg/h	kg/h	ppmw	kg/h
Dist AO	No	6.6	8	0.2	2.3	0.002	0.94
Dist Al	Yes, 50%	8.3	9.2	0.17	2.6	0.97	304	4.1
Dist A2	Yes, 50%	10.4	9.2	0.1	2.6	0.007	1.06	5.2
Dist Bl	Yes, 80%	7.3	8	0.15	2.3	0.82	256.3	5.8
Dist B2	Yes, 80%	8.8	7.7	0.09	2.2	0.007	1.1	7
Ext CO	No	6.6	8	0.2	2.3	6E-07	4E-04	-
Ext Cl	Yes, 50%	11.5	8	1.13	2.3	3E-07	2E-04	5.7
Ext C2	Yes, 50%	12.4	7.5	1.2	2.1	2E-06	IE-03	6.2
Ext DI	Yes, 80%	9.8	6.5	1	1.8	2E-06	IE-03	7.8
Ext D2	Yes, 80%	10.2	6.2	1	1.8	7E-07	5E-04

20185653 prh 20 -07- 2018

Table 2. Comparison of the phenol separation processes; phenol stripping and phenol extraction. Energy characteristics.

	Recycle + phenol conversion	Energy of condenser	water to reactor/ solvent makeup	Steam rate	Steam energy
		kW	kg/h	kg/h	kW
Dist AO	No	1117.8	1060	1750	1014
Dist Al	Yes, 50%	1042	988	1750	1014
Dist A2	Yes, 50%	3273	3107	5153	2987
Dist Bl	Yes, 80%	1042	988	1750	1014
Dist B2	Yes, 80%	3119	2960	4917	2850
Ext CO	No	378	12.3	-	296.8
Ext Cl	Yes, 50%	268	29	-	297
Ext C2	Yes, 50%	726	12.7	-	815
Ext DI	Yes, 80%	266	23.2	-	297
Ext D2	Yes, 80%	793	12	-	895

20185653 prh 20 -07- 2018

It will be obvious to a person skilled in the art that, as the technology advances, the inventive concept can be implemented in various ways. The invention and its embodiments are not limited to the examples described above but may vary within the scope of the claims.

Claims

A process for the preparation of hydrocarbons from a recycled or renewable organic material, wherein the recycled or renewable organic material comprises hydroxy-aromatic hydrocarbon compounds, comprising the steps of:

The process of claim 1, wherein the recycled or renewable organic material comprises more than 0.01% by weight, preferably 0.05% by weight, more preferably greater than 0.1% by weight, of hydroxy-aromatic hydrocarbon compounds.

20

The method of claim 1 or 2, wherein the hydroxyaromatic hydrocarbon compounds are selected from plant-based hydroxyaromatic hydrocarbon compounds such as sterols and lignin and animal fat based compounds such as sterols.

The process according to any one of claims 1 to 3, wherein the recycled or renewable organic material is selected from the group consisting of oils based on lignocellulosic biomass, such as lignocellulose pyrolysis fluid (LPL) and HTL bio-crude oil; crude tall oil (CTO) and its derivatives, such as pine yeast (TOP), tall oil fatty acid (TOFA), distilled tall oil (DTO) and crude fatty acid (CFA); sterol lipid from other fats such as animal fats; the recycled or renewable organic material is preferably crude tall oil (CTO) or pine pitch (TOP).

(Y) treating the purified recycled or renewable organic material in an oil refining process to modify the molecular weight of the feed, remove heteroatoms from the feed, alter the feed saturation, rearrange the feed molecular structure, or use any combination thereof to obtain at least one recycled or reclaimed feed.

The process according to any one of claims 1 to 4, wherein step (b) is carried out by heat treatment of recycled or renewable organic material.

20185653 prh 15 -07- 2019

5 (a) procuring recycled or renewable organic material;

(b) optionally purifying recycled or renewable organic material;

Cc) hydrotreating the recycled or renewable organic material in the presence of a hydrotreating catalyst to form a hydrocarbon stream and phenol-containing effluents, (d) separating the phenols from the and (e) recycling the phenol stream obtained in step (d) to step (c) to increase the yield of hydrocarbons obtained from step 15cc) to give hydrocarbons containing less than 1 wt% oxygen.

A process according to any one of claims 1 to 5, wherein step (b) is carried out by bleaching a recycled or renewable organic material.

The process of claim 6, wherein the hydrotreating step (c) takes place in a continuous hydrogen flow.

The process according to claim 7, wherein the continuous hydrogen flow Fh / feed ratio in step (c) is from 500 to 2000 n-1/1, preferably from 800 to 1400 n-1/1.

The process according to any one of claims 1 to 8, wherein step (c) is carried out at a temperature of 270 to 380 ° C, preferably 275 to 360 ° C, more preferably 300 to 350 ° C.

The method of claim 19, wherein step (y) is hydrogen cracking.

The process of any one of claims 1 to 9, wherein step (c) is carried out at a pressure of 4 to 20 MPa.

A method according to any one of claims 1 to 10,

The process according to any one of claims 1 to 11, wherein the hydrotreatment catalyst in step (c) is a supported Pd, Pt, Ni, NiW, NiMo or CoMo catalyst and the support is zeolite, zeolite alumina, alumina.

A process according to any one of claims 1 to 12, wherein step (c) is performed (c 1) by removing oxygen from the recycled or renewable organic material with hydrogen (HDOdla).

The process according to claim 13, wherein the HDO-catalytic lithium in step (cl) is a sulfated NiW, NiMo or CoMo catalyst.

(Y) is carried out in the presence of a hydrocracking catalyst.

The process according to claim 13 or 14, wherein the HDO is carried out at a temperature of 290 to 350 ° C, a pressure of 4 to 20 MPa and a continuous hydrogen flow.

Wherein the hydrotreatment catalyst in step (c) comprises at least one component selected from group 6, 8 or 10 of the Periodic Table System.

The process of any one of claims 1 to 15, wherein part of the hydrotreated product is recycled in step (c).

The method of claim 16, wherein the ratio of fresh feed to hydrotreated product is 2: 1 to 20: 1.

The process of claim 1, wherein the non-aromatic organic solvent is selected from the group consisting of mesityl oxide,

35 isomethylisobutyl ketone, methyl tert-butyl ketone, methyl tert-butyl ether, methyl isopropyl ketone, 3-heptanone, 2-hexanone and mixtures thereof; preferably the non-aromatic organic solvent is methyl isobutyl ketone.

A process for the preparation of recycled or renewable hydrocarbons comprising the steps of:

[x] making hydrocarbons from recycled or renewable organic material according to any one of claims 1 to 18; and

The process of claim 19, wherein step (y) is hydrogen treatment.

The process of claim 19, wherein step (y) is a catalytic thermal cracking.

The method of claim 19, wherein step (y) is

Oxide and / or silica, preferably N1W / Al2O3, NiMo / AhOs or CoMo / AhOs.

The method of claim 20, wherein step (y) is performed in a light hydrocracking (MHC) processing unit.

The method of claim 20 or 21, wherein the step

The method of claim 19, wherein step (y) is steam cracking.

The process of claim 19, wherein step (y) is isomerization.

25 fluidized catalytic cracking.